Isomerization of pentane



am E5 @46 F, M. McMgLLAN ET AL 393993 I ISOMERIZATIO OF PENTANE Filed Aug. 29; 1941 lnvznors: Frank M. McMHan Patented Jan. 15, 1946 STATES PATENT 2,393,051 lsoMEarzA'rroN or PENTANE of Delaware Application August 29, 1941, Serial No. 408,754

Claims.v (Cl. 2605-6835) This invention relates to the catalytic isomer-i zaticn of pentane.

Pentane is obtained in considerable quantities from natural sources such as crude oil and natural gas, and from the products of many renery operations wherein hydrocarbons are treated at elevated temperatures. Pentane occurring in natural sources consists predominantly, and often exclusively, of the normal or straight-chain compound. The products resulting from renery operations contain the branch-chain compounds in amounts which vary greatly with the nature of the operation. Pentane is, however, more readily andpredominantly available in the straight-chain or nor'- mal form.

lPart of the available pentanes is utilized as blending material in the manufacture of motor fuels and -a part is utilized as starting material I for the manufacture of higher-boiling hydrocarbon materials. Normal pentane is chemically quite unreactive and, in view of its poor ignition* characteristics, is a poor fuel component for internal combustion engines. Its isomer, isopentane, on the other hand, is far more reactive chemically and can easily be alkylated with oleiinic hydrocarbons to produce saturated higher molecular weight hydrocarbons having excellent ignition characteristics. It is, of itself, an exceptionally valuable motor fuel component. Isopentane, furthermore, is a valuable starting material for the preparation of a wide variety of organic compounds containing tertiary carbon atoms. In'view of the vastly superior properties of isopentane over normal pentane, a process enabling the moreefcient isomerization of normalA pentane to isopentane is highly desirable.

lt is well known that the aluminum halides possess the ability to catalyze the hydrocarbon isomerization reaction. These catalysts, however, are also etlective in catalyzing. the decomposition of hydrocarbons. By the term decomposition as used throughout this specicatlon. and the attached claims is meant the rupture of carbon to carbon and/or carbon to hydrogen bonds o f the hydrocarbon molecule to result in the formation of hydrocarbons of lower molecular weight than pentane. Thus, processes have been disclosed wherein hydrocarbon'mixtures having a relatively interact, or react with unconverted components wide boiling range are converted in the presence of an aluminum halide catalyst to hydrocarbon mixtures possessing an appreciably lower boiling range. These processes involve the decomposition of at least a considerable part of the hydrocarbon charge to lighter hydrocarbons and may involve secondary reactions whereby the latter products.

effort has been expended in attempts to control the tendency of these catalysts to catalyze the decomposition oi hydrocarbons and thereby enable the` isomerization reaction to predominate. lin the case of the conversion of normal butane to isohutane, satisfactory processes have been developed. Butane, the iirst member of the isomerizable hydrocarbons, is, compared to its higher homologues, comparatively stable. It may he l treated under relatively lsevere conditions with even highly active isomerization catalysts with only minor amounts of decomposition. Pentane,. however, is particularly prone to undergo decompositlonin the presence of isomerization catalysts. When pentane is treated in some of the isomerlzation processes used heretofore, an appreciable amount ofpentane can, under certain conditions, b e isomerized. The extent to which decomposition unavoidably accompanies the isomerlzation reaction, however, generally acts as a, serious' deterrent to the practical application of these processes vto the isomerization of heptane.v These decomposition reactions are detrimental not' only because they occasion considerable loss of pentane by converting it to undesirable by-products, but because these by-products, even were they to be formed in only relatively small amounts, generally bring about rapid destruction ci catalyst activity. The hitherto proposed isomerization processes, although they may he used for the isomerization of butane, are therefore generally unsuitable for the practical isomerlzation oi7 pentane.

It is an object of the present invention to provide an improved process whereby normal pentane can be converted eillciently to isopentane in the vapor phase without any substantial decomposition of the pentanes.

In accordance with the present invention, normal pentane, in admixture with isobutane, is contacted in the vapor phase with a catalyst comprising an aluminum halide and a porous support material .at correlated conditions of temperature. catalyst activity, and proportion of isobutane to isopentane, whereby normal pentane is isomerized to isopentane without any substantial decomposition of the pentanes. i

The catalyst used inthe process ofthe invention comprises an aluminum halide such as, for example, aluminum chloride, aluminum bromide, or a mixture of aluminum chloride and aluminum bromide in combination with a suitable carrier or support material. Although a great many inert porous support materials such as, for example,

' the following conditions:

fire brick, silica stone, charcoal, pumioe. etc., may suitably be used, it is preferred to use as the support material certain adsorptive'materials `the like, as well as the prepared hydrated materials such as the prepared permutites and zeolites, aluminum oxides, magnesium oiddes, silicas, etc., prepared by partial dehydration of the respective hydroxides and the like, and other aluminous and/or silicious adsorptive materials. A particularly active catalyst comprises a combination of aluminum chloride and adsorptive alumina, and for the purpose of convenience the following detailed description of the invention will be made with reference to this catalyst.

These catalysts are particularly lilfective in catalyzing the hydrocarbon isomerization reaction. However, when they are applied to the isomerization of normal pentane, the isomerization` reaction is generally accompanied by a substantial amount of decomposition, resulting in a rapid decline of catalyst activity. It has now been found that by effecting the catalytic isomerization in the presence of isobutane added in excess of a certain minimum proportion determined by temperature conditions and activity of the particular,

catalyst used, decomposition can be substantially completely suppressed. It has also been found that a substantially higher level of catalyst activity can be obtained and maintained over prolonged periods of operation by control of the concentration of isobutane in the reaction zone.

The proportion of isobutane to pentane to be maintained within the reaction zone may vary within the scope of the invention in accordance with the composition of the particular catalyst used and the operating conditions employed. Maintenance of a substantial molecular excess of isobutane in the reactants is, however, essential to attain substantially complete suppression of pentane decomposition at a high level of catalyst activity, as measured by conversion of normal pentane to isopentane in a single passage of the reactants through the reaction zone. The elfect of yincreased isobutane concentration in the reactants is evidencedby the following examples:

Example I Y Normal pentane was isomerized in the vapor phase in the absence of added isobutane'under Catalyst: Activated alumina impregnated with 22% by weight of anhydrous aluminum chloride Temperature: 50 C.

Pressure: between 15 and 20 p. s. i. abs.

Space velocity: 5 mois n-pentane/liter of catalyst/hour yPromoter: 1 mol per cent lHC1 in hydrocarbon charge.

In this operation severe decomposition of pentane was encountered, resulting in a rapid decline of catalyst activity.

Example II Normal pentane was isomerized in the vapor phase under the conditions of Example I with the exception that isobutane was added to the pentane charge and the partial pressure of pentane was maintained at 20 p. s. i. abs. Under these conditions the space velocity and amount of promoter used were as follows:

Space velocity: 5 mois n-pentane/liter of catalyst/hour 5 mois isobutane/liter of catalyst/hour A Promoter: 1 mol per cent HCl (based on total hydrocarbon feed) isobutane in concentrations slightly in excess of equal molecular proportions with respect to pentane ultimately suppresses the decomposition of pentane when using the above-described catalysts, it does so at a relatively low level of catalyst activity. It has been found, however. that by increasing the concentration of isobutane in the reactants, complete suppression of pentane decomposition at a considerably higher level of catalyst activity is obtained, as shown by the following examples:

Example III Normal pentane was isomerized under the conditions set forth in Example 1I with the exception that the amount of isobutane in the charge was doubled, the partial pressure of pentane being maintained at 20 p. s. i. abs. The space velocity was thenas follows:

5 mois n-pentane/liter of catalyst/hour 10 mois iscbutane/liter of catalyst/hour Isomerization of pentane to isopentane at a high level of catalyst activity in the absence of decomposition was obtained. At the end of thirty hours of continuous operation, a conversion of normal. pentane to isopentane of 50% was obtained, the

rest of the pentane charge remaining substantially unchanged.

Example IV 5 mois n-pentane/liter of catalyst/hour 20 mois isobutane/liter of catalyst/hour Decomposition of pentane was not apparent at any time during the operation and the isomerization proceeded at an exceedingly high level of catalyst activity. Conversions of normal pentane to isopentane as high as 80% were obtained. An

. average conversion of normal pentane to isopentane of -52% was obtained for a period of 390 hours of continuous operation. A

It is seen that the maintenance of a substantial molecular excess of isobutane in the reaction zone not only makes possible the isomer-ization of nor mal pentane in the vapor phase in the absence of pentane decomposition, but enables the isomerization to proceed at an exceedingly high level of catalyst activity. It is furthermore to be noted that the presence of isobutane in substantial molecular excess enables the maintenance of this high level of catalyst activity over prolonged perisubstantially ods of operation. The process of the invention is, therefore, preferably executed in the lpresence of asubstantial molecular excess of isobutane in the reactants and preferably with the maintenance of a molecular concentration of -isobutane to pentane of at least 2 to 1.. It is preferred to maintain the isobutane content of the'react'ants not substantially-in excess of that required to attain the above-described advantageous results. Molecular proportions of isobutane to pentane of from approximately 4 to i to approximately 5 to 1 need generally not be exceeded to obtain the optimum results of the process. It is to be understood, however, that greater concentrations of isobutane, up to, for example, molecular proportions of isobutane to pentane of 7 to l, and even higher, may be used if desired.

' It has been shown that the concentration of isobutane in the reactants influences the level of catalyst activity at which isomerization can be carried out in the absence of pentane decomposition, and that for a catalyst of a given maximum tion of isobutane must be maintained in the reactants to enable the isomerization to proceed at this maximum level of catalyst activity without decomposition-of pentane. Thus, at a high level of catalyst activity, a higher concentration of isobutane is required to suppress. decomposition than at a lower level of catalyst activity.

In the above examples it is shown that at a level of catalyst activity resulting in a conversion' of pentane to isopentane of 50%, a molar ratio of isobutane to pentane of approximately 2 to l was suilicient to suppress decomposition, whereas under the same conditions of operation a catalyst r at a sumciently high level of activity to produce aluminum chloride in combination with adsorptive alumina, an initial molecular concentration of isopentane to pentane in excess oi 2 to l, for

example about 4 to 1, may be maintained and progressively reduced to a molecular proportion .preferably not below approximately l to l, as the activity of the catalyst declines. Care is taken.

to such a degree that a conversion of 'normal pentane 'toisopentane of only 17% was obtained;

l Although normal butane has no substantial effect as a suppressant of the undesired decom- .position reactions, the presence of lesser amountsV of this hydrocarbon is not harmful and it may be present in the reaction zone or in the isobutane. recycled in the system. In carrying out the proc- .level of activity a certain minimum concentraess of the invention on a practical scale, normal butano may be separated from recycled isobutane to any desired degree. The recycled hydrocarbon stream may, however, comprise normal butane and isobutane in relative proportions corresponding approximately to those of the equilibrium mixture at the conditions of operation. ,y I The process of the invention permits the attainment oi exceedingly high conversions at relatively low temperatures, for example not in excess of about 60 C. Although 'it is preferred to' execute the process in this preferred temperature range,

somewhat higher temperatures, for example up to approximately 100 C., may suitably' beused. It is to` be noted that with increase in the operating temperature relatively greater proportions of isobutane to pentane must be maintained to suppress decomposition. I The process may be executed under atmospheric, subatmospheric, or superatmospherlc pressures. Suitable superat mospherlc pressures comprise those enabling maintenance of the reactants in thevapor state at the isomerization temperatures used. Pressures up to, for example, about 150 pounds, have been i'ound to -be suitable.

The method-of the'invention, whereby normal pent'ane is isomerized in the vapor phase without any substantial decomposition of 'pentana lends itself readily to emcient application on a practical scale. The attached drawing shows a more or less diagrammatic elevational view of one form w of apparatus suitable for carrying out the process of the invention. Y

however, that the concentration of isobutane in n the reactants s at all times sumciently high to void any pentane decomposition.

til)

It is to be noted that the unusual edectiveness.

in suppressing decomposition in the vapor phase isomerization of pentane, and in maintaining the high level of activity of the above-described cata lysts, is not possessed by normal butano or propane. The effect of substituting n-butane ici" isobutane is illustrated by the following example:

Example V kPentarie was isomeriaed at'the conditions of- Example IV with the exception that normalv butane was substituted for isobutane. Excessive pentane decomposition was encountered for a period of seven hours.. Thereafter decomposition subsided but the activity of the catalyst had fallen ze: suchaafor example, anhydrous aluminum chloysectional area I9.

chamber is shown in the drawing, it is to bevReferring :to the drawing, normal pentane drawnfrom an outside sourcel is forced by means of pump i@ through linei i, into a suitable heat--l ing zone. 4Isobutane drawn from an outside source, or recycled from within the system as described. more f fully here-below, is passed through line i2, controlled by valve i3, and admix'edwith the pentane charge flowing through line li to the heating zone. The amount of isobutane so introduced into line ii is carefully' a suitable dehydrating medium such as, for example, alumina, calcium chloride-or. the like. In passing through the dehydrating'medium within chambers il, any moisture withinthe hydrocarbon stream is .removed therefrom. From charnbers i'Lthe preheated, dried hydrocarbon stream is passed through line it, into a reaction zone.

The reaction zone may suitably consist of a plurality of tubes or a chamber of restricted cross- Although but one reaction understood that more than'one such chamber, in series or parallelvapor communicationl with one another, may suitably be used. A 'suitable isomeriz'ation catalyst of the typev described above ride in combination with adsorptive alumina, is

.maintained within reaction chamber i3. Temperature conditions within the above-described range of temperatures `suitable for isomerizing `normal pentane in accordance with the invention are maintained in chamber I8 by control of the heat input into heat exchanger l5. In passing through the catalyst within reaction chamber I8 under the prescribed conditions, normal pentane is isomerized to isopentane without any substantial decomposition of the pentanes at a high level of catalyst activity.

The isomerization, when employingv catalysts of the above type, is preferably effected in the presence of a hydrogen halide such as, for exlample, hydrogen chloride. This is preferably -introduced into the reaction chamber with the hydrocarbon feed. Hydrogen chloride is therefore drawn from an outside source through line 2n,

provided with valve 2i, leading into line i2. Thev amount of hydrogen chloride introduced into the system may vary widely in accordance with the catalyst composition and the operating conditions line 23 may be passed directly into line 85. should rthisbenieuwd.

employed. The hydrogen chloride introduced into line I i may amount to, for example, from 0.3% to approximately of the pentane charge.

A mixture comprising isopentane, unconverted normalpentane, isobutane, hydrogen chloride,

and any normal butane which may have been formed by the isomerization of isobutane, is withdrawn from reaction chamber i9 and passed through line 22 into accumulator 23. A cooler 24 is positioned in l line 22. In passing through cooler 24, the stream is cooled to a temperature at least suiiiciently low to eeot the condensation of the pentanes. If desired, additional cooling or 'refrigerating means may be provided to aid in cooling'a the stream flowing through line 22. Accumulator 23 is provided with a vent 25 to permit elimination therefrom of any gaseous productsiif this should be desired during the course of the process. .Vapors and gases comprising hydrogen chloride and C4 hydrocarbons are drawn from accumulator 23 through line 26 to compressor21. From the high pressure side of compressorl 21; the stream is passed through line 28 into a fraccoils 56 and 51, are `providedin the lower part a) treatment. Thus, unsaturatedhydrocarbons mayv v tionator 29. Liquid comprising C4 and Cs hydrothrough line 35, controlled by valve 3l, to line' I2. A heat exchanger 31 is positioned in line 35 to permit indirect heat exchange between the gaseous stream flowing through line 35 and the hot reaction products emanating from chamber I9. If desired. a part or all of the gaseous stream taken overhead from fractionator 25 may be subjected to any desired additional fractionation to separate any constituents such as. for example, normal pentane, therefrom prior to recycling the stream through line 35., 'I'he hydrogen chloride and isobutane separated from thereaction products may be recycled to the reaction zone in separate streams by means not shown in the drawing. By means of line 33, provided with valve I. at least a. part of the gaseous stream flowing through tane of at least 4:1, progressively reducing the Liquid, comprising c hydrocarbons, is wun-` drawn from the bottom of column 29 and passed through line 40, controlledv by valve 4|, into a second fractionator 42. Within fractionator 42, a vapor fraction comprising isopentane is separated from a liquid fraction comprising normal pentane. 'I'he vapor fraction is withdrawn from the top of fractionator 42 and passed through line 43 and cooler 44, into an accumulator 45. In passing through cooler 44, the stream is cooled to a temperature sufficiently low to effect the condensation of isopentane. Liquid comprising isopentane is withdrawn from accumulator 45 through line 4B, provided with valve 41, as the desired product of the process. A part of the liquid flowing through line 48 is forced by means of pump 48 through line 49. as reflux, to the upper part of fractionator 42. Liquid. comprising normal pentane, is withdrawn from the lower part of fractionator 42 through line 5l, controlled by' valve 52, and eliminated from the system. At least a part of the liquid comprising normal butane flowing through line 5I is forced by means of pump 53 through line 54 into line Il.

Fractionator 23 is provided with suitable cooiing means in the upper part thereof such as, for example, a' closed cooling coil 55. Suitable heatingmeans such as rebollers or closedheati'ns of fractionators 2l and 42, respectively, to aid in eifecting the desired fractionation therein.

p The pentane 'and isobutane charged to the system are preferably substantially free of any materials which are prone to undergo undesired reactions at the operating conditions. Such im'- purlties, if present in the hydrocarbons` charged, may be removed therefrom by any suitable prebe eliminated by a pretreatment such as ac i v treating, hydrogenation, or the like.v c

We claim as our invention: l 1. In a process for lsomerizing normal pentene to isopentane wherein normal pentane vapors in admixture with added isobutane are contacted at' y y a temperature not exceeding about 60 C. with a cataiystcomprising aluminum chloride in combination with adsorptive alumina whereby said catalystv declines in activity as. the operation proceeds, the improvement which comprises maintaining an initial molar ratio of isobutane to penratio of isobutane to pentane to a minimum molar ratio 012:1 as the activity of the catalyst declines, and controlling said progressivereduction of isobutane to maintain the ratio of isobutane to pentane at all times suiliciently high within said prescribed range to eect the conversion of normal pentane to isopentane in the absence of any substantial hydrocarbon decomposition.

2. In a process for isomerizing normal pentane to isopentane wherein normal pentane vapors in vadmixturev with added isobutane are contacted at isomerizing conditions with a catalyst comprising aluminum chloride in combination with adsorptive alumina whereby said catalyst declines in activity as the operation proceeds, the improvement which comprises maintaining an initialv molar ratio of isobutane to pentane` ot at least 4:1, progressively reducing the ratio of isobutane to pentane to a minimum molar ratio of 2:1 as the activity of the catalyst declines, and control-v ling Asaid progressive reduction of isobutane to maintain the ratio of isobutane to pentane at all prising an aluminum halide in combination with y adsorptive alumina whereby said catalyst declines in activity as the operation proceeds, the improvement which comprises maintaining an initial molar ratio of isobutane to pentane of at least 4:1, progressively-reducing the ratio of isobutane to pentane to a minimum molar ratio of 2:1 as

the activity of the catalyst declines, and controlling said progressive reduction of isobutane to maintain the ratio of isobutane to pentane at all times sufiiciently high within said prescribed range to eiiect the conversion of normal pentane to isopentane in the absence oi any substantial hydrocarbon decomposition. y

4. In a process for isomerizing normal pentane to isopentane wherein normal pentane vapors in admixture with added isobutane are contacted at a temperature not exceeding 100 C. with a catalvst comprising an aluminum halide in combination with an adsorptive material whereby said catalyst declines inactivity as the operation 'proceeds, the improvement which comprises maintaining an initial molar ratio oi' isobutane to pentane or at least 4:1, `progressively reducing the ratio of isobutane to pentane to a minimum molar` ratl of 2:1 as the activity of the catalyst declines, and controlling said progressive reduction of isobutane to maintain the ratio of isobutane to pentane at all times sufficiently high within said prescribed rangeto effect thel conversion of normal pentane to isopentane in the absence of any substance hydrocarbon decomposition.

5. In a process for isomerizing normal pentane to isopentane wherein normal pentane vapots in admixture with added isobutane are con- Y tacted atisomerizing conditions with a catalyst comprising an aluminum halide in combination with an adsorptive material whereby said catalyst declines in activity as the operation proceeds, the improvement which comprises maintaining an initial molar ratio of isobutane to Dentane of at least 4:1, progressively reducing the ratio of isobutane to pentane to a minimum molar ratio of 2:1 as the activity of the catalyst declines, and controlling said progressive reduction of isobutane to maintain the ratio of isobutane to pentane at all times suilicientiyhigh within said prescribed range to eiect the conversion oi' normal pentane to isopentane in the absence of any substantial hydrocarbon decomposition. 

